ES2466165T3 - Catalytic gasification - Google Patents

Abstract

A gasifier (1) for the gasification of biomass and waste to produce a fuel effluent, comprising: a) a fuel valve (22), for loading solid fuel (11) into a first oxidation zone (8); b) a first throat (2), which defines the lower edge of the first oxidation zone (8); c) a second throat (4), which defines the lower edge of a second oxidation zone (14); d) a reduction zone (5), which joins the first oxidation zone (8) with the second oxidation zone (14); and e) two vortex discharge tubes (18), located opposite (in the reduction zone), for the fuel effluent; wherein the gas flow in the first oxidation zone takes place in the same direction as the fuel flow, and the gas flow in the second oxidation zone takes place in the opposite direction to the fuel flow, and which is characterized by that below the reduction zone (5) there is located a zone (3) with a microporous catalyst, in the form of a perforated jacket (3) for catalysis, which joins the first oxidation zone (8) with the discharge tubes (18 ).

Description

Catalytic gasification

Detailed Description of the Invention

The present invention relates to a gasifier, and a method of operation of the gasifier, to produce a  fuel effluent

Gasifiers are used in the gasification of biomass, fossil fuels and waste, either separately or mixed together, to produce a variety of combustible gases that can be used to generate energy, for example, through the use of internal gas combustion engines, gas turbines, diesel engines dual fuel and fuel cells.

 The interest in the use of gasifiers for the treatment of residual products is increasing due to the increase of the cost of waste disposal by conventional methods, such as incineration or deposit in landfills, driven by environmental concerns associated with these methods.

Typically, conventional gasifiers operate in batch mode, where slag formation and carbon, as well as the formation of bridges, creates an intermittent gas and a flow of fuel that, in turn, is  Associates with a product gas with a high tar content. On the other hand, the carbon formed during the Gasification procedure cannot be discharged effectively, due to the relatively high temperatures premises in the oxidation zone. Gasification of fuels with a high ash content can lead to discharge into the gasifier of high carbon waste, which can then be difficult to remove. As a result of these difficulties, conventional gasifiers are operated until the

 complete gasification of the fuel, and then stop in order to manually remove the slag and carbon formed in the high temperature regions of the gasifier, together with the high carbon ashes.

An additional problem comes from the batch operation of the gasifiers, because the operating conditions Undesirable occur during the start-up phase, and if the gasifier operates at low temperatures (<850 ° C) During normal use, the tar content of the product gas may increase. The tar of the product gas is

 deposits inside the combustion device used to burn the product gas, blocking the device and requiring cleaning. Current energy and heat production devices, which normally they are incorporated in the gasifiers, they are not suitable for the use of a product gas charged with tar and moisture.

In the present invention it has been found that many of the difficulties of known gasifiers are due

 here the gasifier has two oxidation zones, where the flow of gas in the first zone takes place in downward direction (in the same direction as the fuel flow), and in the second zone, below the First, the gas flow takes place in the upward direction (in the opposite direction to the fuel flow). Yet such device can be called `` down-ascending gasifier '' to reflect the combination of the gas flow down and up.

 Therefore, a first aspect of the present invention provides a gasifier for the gasification of a solid fuel to produce a fuel effluent, comprising a fuel valve to load the solid fuel in the first oxidation zone, a first throat that defines the lower edge of the first oxidation zone, a second throat that defines the lower edge of the second oxidation zone, about air admissions for both oxidation zones, a reduction zone that joins the first oxidation zone

 with the second oxidation zone, and two vortex discharge tubes located opposite (in the zone of reduction) for the fuel effluent, where in the first oxidation zone the gas flow takes place in the same direction as the fuel flow and in the second oxidation zone the gas flow takes place in direction opposite to the flow of fuel, and being characterized by that below the reduction zone this located an area with a microporous catalyst, in the form of perforated jacket for catalysis, which joins the first

 oxidation zone with discharge pipes.

In a particular advantage, the gasifier is suitable for continuous operation and the method is a method of continuous operation capable of operating for prolonged periods, without stopping to eliminate slag and the charcoal This is because a high degree of gasification takes place, due in part to the uniformity of the gasification and also the ability to remove ashes and slag from the base of the gasifier during the

 operation. An additional advantage is the minimization of the hours of operation in the starting node, mode in the which tends to increase the tar content in the product gas.

In the gasifier of the invention, the first oxidation zone preferably operates at a temperature of at least 1,000 ° C, while the reduction zone operates at a temperature between 600 and 900 ° C, more preferably at approximately 850 ° C, and the second oxidation zone operates at a temperature between 700 and 800 ° C, plus

 preferably at about 750 ° C. This ensures the uniformity of gasification.

It is preferred that the gasifier of the invention also comprises a pyrolysis zone above the first oxidation zone, and a fuel storage zone above the pyrolysis zone. In the use of such a gasifier, in a preferred method of the second aspect of the invention, the fuel is dried in the area of fuel storage and pyrolysed in the pyrolysis zone, to produce a pyrolized carbonaceous material

 (quot; charcoalquot ;, in English) which is then partially oxidized, reduced and further oxidized. Storage area and / or fuel drying preferably operates at a temperature between 80 and 120 ° C, and more preferably at approximately 100 ° C. The pyrolysis zone preferably operates at a temperature between 500 and 700 ° C, plus preferably at about 600 ° C. The heat needed to maintain these temperatures comes from the Main oxidation zone.

 Preferably, the fuel storage zone comprises a hopper that has a loading valve and which leads to a grill above the first oxidation zone.

The perforated jacket allows the effluent gas, produced in the gasification process, to be cleaned and disposed of effectively, reducing its trajectory through the second oxidation zone.

The gasifier of the first aspect of the invention also preferably comprises means incorporated into the

 discharge tube to keep the gasifier below atmospheric pressure, so that the air is sucked into gasifier through appropriate air inlets. The operation of the gasifier below the pressure atmospheric provides a fail-safe mechanism, so that, in the event that the means to fail keep the pressure reduced, the combustion processes in the gasifier stop abruptly due to the lack of oxygen, avoiding a dangerous accumulation of product gases.

 The air inlets to the gasifier are maintained with negative suction through the main pipes of air entrance. The aspirated air is continuously withdrawn through the annular ducts that are located in the outer circle of oxidation zones. The annular ducts provide the air to be preheated, before its injection into the reaction zones through air intake nozzles mounted on the internal surface of the sloping throats. Therefore, preheated air also has a cooling effect for surfaces.

 Metallic gasifier at the level of the throats.

In the gasifier of the present invention, the amount of secondary oxidation in the second oxidation zone is controls by the amount of air admitted by the secondary air intake valve.

Such a gasifier can be used to gasify solid fuels, including biomass, fossil fuels, waste or combinations of the same, to produce a fuel effluent. The "solid fuel"; may  contain entrained liquids (such as moisture, oil, oil sludge) inside the intra or interparticle pores of solid ° fuel particles.

Therefore, a second aspect of the present invention provides a method for the gasification of solid fuel to produce a fuel effluent, which uses a gasifier of the first aspect of the invention, comprising the steps of partially oxidizing the solid fuel in the first oxidation zone for

 produce a pyrolized material (quot; charquot ;, in English), reduce the pyrolized material in the reduction zone to form ashes, further oxidize in the second oxidation zone any residue of pyrolized material in the ashes and extract the fuel effluent produced in the previous stages by means of the discharge pipe, where in the first oxidation zone the gas flow takes place in the same direction as the fuel flow and in the second oxidation zone the gas flow takes place in the opposite direction to the fuel flow.

 Preferably, the fuel effluent produced in both zones at a temperature of about 850 ° C passes through a perforated conical ring that is filled with a microporous catalyst to crack the tars residuals, just before leaving the gasifier.

Preferably, the solid fuel for the gasifier and the method according to the invention incorporates biomass, such as liquid waste, residual oils or oil sludge, or fossil fuels or waste or

 combinations thereof, as defined above, which are absorbed into the pores intraparticle and interparticle of a suitable fuel vehicle. Preferably, the fuel vehicle it has a high internal porosity and more preferably it is in fibrous form to provide a wide porosity interparticle Preferably, the liquid residue is mixed with the vehicle and briquetted in order to densify the composite fuel.

 The biomass that can be gasified by the gasifier and the method of gasification of the invention may include any of the extremely varied conventional sources, and includes, for example, wood and lignocelluloses, sawdust, carbon, nutshells, sewage sludge, leather waste, waste plastic and plastic, urban waste or domestic residual materials, olive bones, flour rapeseed, clinical waste, garbage and manure from polio and livestock, waste from nnataderos, waste from

 Bitter chocolate, tallow, paper waste, food waste, sugarcane bagasse, residual oil, sludge of petroleum, carbon fines, bone waste, agricultural waste and biomass mixtures with fossil waste, such as oil sludge mixed with bone waste, sewage sludge, sawdust or flour rapeseed seeds

A suitable vehicle can be selected from sawdust, crushed bone waste from slaughterhouses, bread / food waste, urban waste, dry sewage sludge, chopped straw, seed meal rapeseed and calla de azilcar bagasse.

It is preferable to use briquettes or fuel pellets (such as biomass or residual carbonaceous materials) of

 uniform schedule to achieve a uniform distribution of air during gasification. It is also preferable that the maximum diameter of the fuel briquettes is not greater than one eighth of the narrowest part of the gasifier, to avoid the formation of bridges.

In the gasification method, the amount of secondary oxidation required depends on the material content Pyrolized remaining in the ashes of fuels. In conventional gasifiers, fuels with

 high ash content, such as sewage sludge, leather waste, oil residue sludge, domestic waste (RDF), bone meal, chicken manure and cattle, generally result in a low carbon conversion because the ashes isolate part of the carbon in the main oxidation zone.

It is described here below, but without being part of the claimed invention, a gasification system that it comprises, in series: the gasifier of the invention, a water washer, a polymer filter unit, a

 fan, an additional polymer filter unit and means for the output of the product gas for power generation, such as an effluent chimney that leads to a location for an ignition clean.

Preferably, the system comprises a bypass of the filter for use during startup. Preferably, the filters comprise double filter units, which each operates in tandem, so that it only operates at  same time in the filtering mode one of the halves of each double filter unit, operating the other half in the regeneration mode.

In a further aspect of the unclaimed invention there is provided a method for operating a system of gasification as defined above, which comprises gasifying a solid fuel as defined previously, pass the product gases through a scrubber to clean them of particles and toxins

 soluble in water, as well as acids, a filter to absorb tar and moisture, a fan to accelerate gases, a second filter to absorb additional tar and moisture, to produce an ignition gas clean. In order to remove the acids from the gas, the pH of the water washer is low.

Preferably, the gas from the water washer does not pass through the first filter during start-up. Preferably, the gas is filtered at the same time in each of the halves of the double filter unit, being

 regenerating the other half, most preferably with hot exhaust gases. In a particular advantage, the gas leaving the fan is at a high pressure, which leads to additional condensation of the tar and the moisture in the second polymer double filter unit.

In an additional advantage of the invention, the system of the invention and the method for its operation produces a gas that is suitable for energy and heat production devices, which has a low content  tar and moisture, and preferably is substantially free of tar and moisture.

It has now been found that the extraction of moisture and tar can be further improved with the use of a Open cell microcellular polymer filter.

Accordingly, in a further aspect of the invention a polymer filter is provided comprising a polyHIPE open cell microcellular polymer comprising pores in the range of 0.1 to 300

 micrometers (primary pores) and, optionally, additionally in the range of 300 to 10,000 micrometers (pores coalescing), where the polymer is effective for the absorption of water and tar in gases, and a method for the preparation thereof.

As the water-absorbing materials, both the acid and neutralized salt form of the sulfonated microcellular polymers (which are also known as PolyHIPE polymers).

 These polymers are prepared using the settling of our previous patent application, (polymers microcellular as cell growth media and new polymers, EP-1183328, US Pat. N ° 09 / 856,182). For water absorption it is possible to use polymers with primary pores and, optionally, additionally coalescing. These types of pores are described below:

Primary pores in the range of 0.1-300 pm; for example, pores of tame * small: 0.1-0.5 pm and pores of  large size: 0.5 to 300 pm.

Coalescing pores in the range of 300-10,000 pm. Preferably, the coalescing pores have a size of pores in the range of 300 to 1,000 pm.

Using the methods quo described below, a polyhipe polymer with a diameter of particular pores In open cell polymers, intercellular communications are known as

interconnections. A polyHIPE polymer can have any desired relationship between the diameter of the interconnections (d) and that of the pores (D), for example in the range 0lt; d / Dlt; 0.5, preferably in the range 0.1lt; d / Dlt; 0.5 when the pore diameter is approximately less than 200 micrometers. Interconnections they can have a diameter in the range of up to 100 micrometers, preferably 0.001 to 100 micrometers, more

 preferably 1-50 micrometers.

Commercially available polyhipe ester polymers or can be prepared using the methods that are described in US Pat. No. 5,071,747 and in the additional patent publications referred thereto or which described later.

The commercially available generic ° polyhipe polymer comprises a polyvinyl polyhipe polymer and is

 It consists of oily-phase styrene monomers, divinylbenzene (DVB) and a surfactant (monooleate sorbitan Span 80), and can be rigid or flexible depending on the relative proportions of the monomers, additionally including in the flexible form the monomer ° of 2-ethylhexyl acrylate, and in the phase aqueous an amount of potassium persulfate as an initiator of the aqueous phase.

However, due to the presence of sulfur in the polymer, its use in gas cleaning may not be  desirable for the environment. Therefore, it is preferred to use other forms of microcellular polymers.

When the use of sulfur groups in the polymer is undesirable, it is preferable to use oil phase initiators such as lauryl peroxide (1% of the oil phase).

Therefore, a first new polyHIPE polymer comprised in a filter of the invention incorporates an initiator of the oil phase, preferably 1,1-azobis (cyclohexanecarbonitrile) or lauryl peroxide in 1% of the oil phase of the  emulsion.

A second new polyHIPE polymer comprised in a filter of the invention incorporates a monomer (such as the 2-vinylpyridine) to make the polymer adsorbent without causing the emulsion to break, being present preferably in an amount of 5-10%. The new polymers can additionally incorporate a monomer ° (such as 2-ethylhexyl acrylate) to incorporate elasticity and improve mechanical shock absorbency and some

 Good abrasion characteristics. The elasticity is also Citil to improve the capacity of water uptake of the hydrophilic polymer. The preferred value of the 2-ethylhexyl acrylate concentration is up to Y = 30%, but more preferably Y = 15%.

A third new polyHIPE polymer comprised in a filter of the invention incorporates a vinylpyridine monomer (with or without a 2-ethylhexyl acrylate monomer) in the form of a skin-core polyhipe structure, in which the

 nude ° of the polymer is sulphonated but the skin is not sulphonated, although in spite of this it is adsorbent of the water. This is done by injecting in the nude ° of the polymer a small amount of acid ° sulft: wico and, subsequently, sulfonate this polymer using known methods. This ensures that the sulfur-containing part be encapsulated, but still a part of the polymer can adsorb water.

It has been discovered that polymers should not be dried excessively during the "drying stage". A drying

 excessive results in the reduction of the water absorption capacity of the polymer, as well as the reduction of the water catchment rate. Typically, the water absorption capacity of these polymers is 10-12 times their own weight

The polymer of the invention can be natural or synthetic, soluble or insoluble, optionally it can be a polymer biodegradable crosslinking, preferably selected from proteins and cellulose, polyacrylamide,

 rigid or flexible polyvinyl, poly (lactic acid), poly (glycolic acid), polycaprolactone, poly (lactide / glycolide) and polyacrylamide.

In a first stage, the process for the preparation of microcellular polyhipe polymers comprises the formation of an emulsion of high internal phase (HIPE) of the dispersed phase in the continuous phase, where the phase dispersed may be empty or may contain dissolved or dispersed materials, and in the continuous phase they are present

 monomers, oligomers and / or prepolymers, homogenization and polymerization thereof, by means of introduce the dispersed phase in the first stage through controlled dosing in the continuous phase, with controlled mixing at controlled temperature, to achieve an emulsion, and then homogenize during a controlled period under controlled deformation and polymerization, under temperature conditions and controlled pressure.

 Type-1 pores (base pores): This is the basic structure of the pores whose schedule is determined at the stage of emulsification of PHP training. Therefore, the pore size is mainly determined by the history of deformation (flow) of the emulsion. The integrity of these pores is maintained during polymerization and at this stage the interconnections are formed. Depending on the chemical composition of the oil and water phases, The volume of the phases and the polymerization conditions, such as temperature and pressure, can be

 control the size of the interconnections in the range 0lt; d / Dlt; 0.5.

Type-2 pores (coalescing pores): This type of pore architecture is obtained by tray & coalescence controlled of type 1 pores during polymerization. The droplets of the dispersed phase in the PHP emulsion they are fused by adding to the aqueous phase of water soluble polymers, or by adding to the phase oil of slightly hydrophilic oils (such as styrene oxide) or by raising the

 concentration of the monomers in the emulsion. In this case, the tame () of the interconnections is the same as the of the pores of type-1 that form a matrix that incorporates the fused pores. However, the d / D ratio is very small due to the fact that the fused pores are very large compared to the base pores.

Very small pore size emulsions (0.1 to 0.5 pm) are obtained using very high flows strain rate where the flow is predominantly extensional and the emulsification temperature is  as low as possible. Tame ° emulsions of large pores (0.5 to 300 pm, for example close to 200 pm) are obtained at high temperatures and just above the critical deformation rate, below which The emulsion is totally or partially reversed, for example, for an oil-in-water type system. For a system given, the critical strain rate can be determined by, for example, the variation in the speed of addition or strain rate during mixing. These emulsions should also be treated in a short

 period of time, using predominantly shear flows.

Very large pore emulsions (300 to 10,000 pm, preferably up to 1,000 pm) are obtained during the polymerization through the controlled pore coalescence method. There are two methods to get the controlled coalescence: 1) by adding to the aqueous (dispersed) phase a known amount of polymer soluble in water, or 2) by adding to the continuous oil phase solutes of material from "cargo". In both

 methods, the concentration and type of these additives is important. If the concentrations are low, these additives they give rise to polyhipe polymers with pores in the range of 1-200 pm with some desired properties. If the Concentration is above a certain value, coalescing pores begin to form. In this case, the Pore size is determined by the pore size before the start of coalescence, the temperature of polymerization and concentration, molecular weight and type of additive.

 The emulsion can be obtained from any desired immiscible phase that forms a continuous and dispersed phase, preferably from aqueous and non-aqueous phases, more preferably from aqueous and oily phases. The Emulsion obtained can be an aqueous emulsion in oil or an emulsion of oil in water.

By means of the controlled dosing of the dispersed phase in the continuous phase, it is possible to achieve the emulsion desired. In a batch mixer, the dosage of the dispersed phase is preferably carried out from the part

 bottom of the mixer, using single or multiple entry points. Ticket feeding Multiple resulted in emulsions of larger pores. If the dosage rate was very fast, the mixing created by the emerging water phase jet was too intense and, therefore, the pore tarnario of the emulsion. Therefore, the combination of multiple feeding points with a relatively dosing prolonged created an emulsion of large pores. After the completion of the dosage, the emulsion was taken  than homogenize, but the pore size () decreased if the homogenization period was long.

Controlled mixing as defined above may be critical or extensive. The critical mix is sufficient mixing to cause dispersion of the aqueous phase in the oil phase without phase inversion. The Critical mixing is obtained by using a honnogeneous mixing field in which the pore size It is substantially uniform, which avoids the breaking of the emulsion and the reversal of phases.

 Mixing can be done by any suitable means to provide a mixing field. substantially homogeneous throughout the volume of the two phases, and preferably mixing is performed by multiple blades, multiple nozzles and the like.

Contrary to the teaching of US Pat. No. 5,071,747, it has been previously found that the Achieving a stable emulsion with a large pore diameter is achieved by minimizing intensity  of mixing. Consequently, by means of a dosage, a homogeneous mixing and the like, You can obtain a stable emulsion regardless of the need for intense mixing. The homogenization can be carried out in an external loop using a pump, such as a pump gears or a screw pump, which can also be connected to a static or dynamic mixer. Some Types of static or dynamic mixers suitable for this type of homogenization are described in: Akay,

 G .; Irving, GN; Kowalski, A.J .; Machin, D. Dynamic mixing apparatus for the production of liquid compositions. U.S. Patent No. 6,345,907, February 12, 2002, and Akay, G. Method and apparatus for floating processing materials and microporous polymers. International patent application. PCT Publication WO 2004/004880, 15 January 2004.

Dosing, emulsification and homogenization can be performed at any suitable temperature,

 depending on the pore size of the final Polyhipe polymer. If the desired pore size is large, the preferred temperature is high, although, nevertheless, below the boiling point of the point phase of lower boiling. When the aqueous phase is the lowest boiling point phase, it boils at about 100 ° C It has been found that the process of the invention, which employs an emulsification temperature of 60 ° C or higher, results in the obtaining of polymers having a pore size greater than 60 micrometers. He

an increase in the emulsification temperature per enclosure of 60 ° C results in a dramatic increase in the size of pores in an amount greater than that achieved by a similar increase in temperature below 60 ° C.

The maximum emulsification temperature may be higher than the normal boiling temperature of the phase of low boiling point, for example, the lowest boiling point phase may include any

 suitable component adapted to raise the boiling point. Preferably, the aqueous phase includes a electrolyte that is stable at 100 ° C and is potentially inert. This means that, preferably, the procedure it is carried out at high pressures when the temperature is above the boiling point of the monomer. The preferred temperature range for high pore tamatium emulsions is 70-110 ° C.

Emulsification and subsequent pollination can be carried out at temperatures above the point of  normal boiling of the materials of the aqueous or continuous phase, by increasing the pressure above the atmospheric pressure using continuous closed circuit treatment equipment.

The process can be carried out by the use of additional aqueous or oil phase initiators, crosslinking agents, fillers and the like, and it is preferred that these are temperature stable maximum operation as defined above. The selection of initiators, crosslinking agents and

 Similar is done with reference to the acceptable viscosity of the phases to be emulsified and homogenized. Can be acceptable to reduce the amount of crosslinking agent required by using a proportion of partially crosslinked prepolymers and prepolymers, optionally with the use of a suitable filler material of the oil phase to increase the volume of the oil phase and reduce the effective viscosity.

Preferably, the process of the invention is characterized by the use of an oil phase initiator, together

 with, or instead of, an aqueous phase initiator as is known in the art. The initiators of the aqueous phase they can be used for operation at lower temperatures, and include sodium or potassium persulfate. For operation at elevated temperature above 80 ° C, oil phase initiators are preferably used, for example, 1,1-azobis (cyclohexanecarbonitrile) or lauryl peroxide.

The crosslinking agent may be, for example, divinylbenzene (DVB). If the polyhipe polymer is required

 be biodegradable, hydrolysable crosslinking agents can be obtained. These crosslinking agents are the ethylene diacrylate, N-N'-diallyl-tartardiamide, N-N (1,2-dihydroxyethane) -bis-acrylannide, and N-N'-Nquot; -trialylcitrictriamide. However, in this case of biodegradable crosslinking agents, the polymer itself must be biodegradable. These polymers are poly (lactic acid), poly (glycolic acid), poly (E-caprolactam) and polyacrylamide

 When water soluble polymers are needed to form the microcellular structure, they must be crosslinked In the case of such polymers, the monomer (such as acrylamide) dissolves in water and forms a HIPE emulsion by dosing this monomer solution in a hydrocarbon liquid, such as hexane or toluene, in presence of a suitable surfactant, initiator and crosslinking agent.

Proteins and cellulose can also form microcellular structures. In this case, these materials, together

 with a suitable emulsifier, they dissolve in a suitable aqueous phase (water for proteins and reagent of Schweitzer, Cu (NH3) 4 (OH) 2, for cellulose) and dosed in a hydrocarbon liquid to form a HIPE Continue in water. Crosslinking is achieved by immersing the HIPE in a glutaraldehyde solution (for proteins) or in an acid solution (cellulose).

The procedure may include the introduction of any suitable modifier, as defined

 before, before or after polymerization. For example, modifiers can be introduced in the phase aqueous dispersed and dosed in the continuous phase as defined above. Alternatively, it is used a post-polymerization modification step, which can simply take the form of a removal of the surfactant, the electrolyte and the unreacted monomer, a coating, a polymerization or a additional reaction on the surface of the existing polymer. Modifying agents and techniques are known in the art.  demodification

As is known in the art, polymerization is carried out under known conditions of time and temperature. for the respective monomer, oligornero or prepolymer to polymerize.

Preferably, the polymer is polymerized in individual molds, so that a skin is formed. This has the advantage of preventing polymer abrasion during use in a single compact. The alternative method of cutting  of the polymer in filler material can lead to its fragmentation into small particles.

In a further unclaimed aspect there is provided a polyHIPE polymer comprising a polyhipe polymer polyvinyl and is composed of oily phase styrene monomers, divinylbenzene (DVB) and a surfactant (sorbitan span 80 monooleate), which additionally incorporates a monomer (such as 2-vinylpyridine) for make the polymer adsorbent to water without causing the emulsion to separate, which is preferably  present in an amount of 5-10%, and / or a monomer (such as 2-ethylhexyl acrylate) to incorporate elasticity and improve the absorbency of mechanical shock and good abrasion characteristics; That characterized in that the polymer comprises pores in the range of 0.1 to 300 micrometers, for example 0.1

at 0.5 micrometers up to 200 micrometers, as primary pores and, optionally, additionally some coalescing pores in the range of up to 10,000 micrometers, for example up to 1,000 micrometers, if the Co-monomer concentration is high.

In a further aspect of the invention, the use of a gasifier, and a method for gasification of gasification is provided.

 solid fuel as defined above, preferably to generate combustible gases for its use in power generation, for example through the use of internal gas combustion engines, gas turbines gas, dual fuel diesel engines or fuel cells.

With reference to the following drawings, a detailed embodiment of the invention is described, as well as some Additional preferable features:

 Figure 1 is a schematic diagram showing our gasifier in accordance with the present invention.

Figure 2 is a schematic diagram showing a gasification system with the gasifier used in the Figure 1 in accordance with the present invention.

The gasifier 1 shown in Figure 1 can be subdivided into five general zones. At the upper end of the gasifier, where the fuel is introduced by means of a rotary valve 22 of upper fuel with  clogging of the air passage, this zone 6 of storage and drying of fuel. Below this area This is the pyrolysis zone 7.

The first oxidation zone 8 is below the pyrolysis zone 7 and the air is supplied through of the air intake nozzles 12 located in the first air distribution throat 2, which defines the lower edge of the area, and at the top of the reduction zone 5. This throat is inclined at an angle of

 10 to 40 °, preferably approximately 20 °, in order to facilitate fuel flow down the gasifier, and may be curved as shown. An angle greater than 40 ° leads to a fuel flow limited. The throat 2 is rigidly welded to the internal surface of the gasifier 1.

The central set of air nozzles 24 can facilitate the distribution of air in the first oxidation zone, and is particularly useful when the throat diameter exceeds approximately 0.5 meters. Preferably a  such nozzle is located in the center, above the first throat 2 of air distribution. The air is supplies the air intake nozzles 12 from the annular conduct 23 formed between the first throat 2 of air distribution and the outer casing of the gasifier. Air is admitted into this annular duct 23 by means of a primary air intake valve 9. If the central set of air nozzles 24 is present, it will be It supplies air from a valve 25 whose operation is connected to that of the air intake valve 9

 primary.

In a gasifier where there is no central set of air nozzles 24, it is preferred that approximately two thirds of the air intake nozzles 12) located on the surface of the inclined throat 2 and that the other East third located in the reduction zone 5, at least 20 cm above the perforated part 3 (see more ahead). If a central set of air nozzles 24 is present, then at each location a

 n Equal number of nozzles.

The throat 2 leads to the reduction zone 5, which descends like a conical tube to the second zone of oxidation 14. The cylinder circumscribing the reduction zone 5 has a part of the perforated housing for catalysis 3, in order to clean and allow the evacuation of the product gas 13 directly to the second oxidation zone at the level of the gas discharge tube 18. The angle that forms the perforated housing 3 stops catalysis with the direction

 vertical is 10 to 40 °, preferably approximately 20 °.

The second oxidation zone 14 is supplied with air 15 through air nozzles 17 which are located in the second air distribution throat 4, which defines the lower edge of the area. This throat is also this inclined an angle 16 from 10 to 40 °, preferably approximately 20 °, in order to facilitate the flow of fuel, and similar considerations apply here for the angle of inclination of the first throat 2 of the distribution of

 air. The throat 4 is rigidly welded to the inner surface of the gasifier 1, and preferably this aligned, or more preferably it is symmetrical, with respect to the first throat 2 of air distribution. The expression quot; symmetricaquot; how it is used here means that the two throats 2 and 4 have the same shape and are located around a common vertical axis.

Air is supplied to the air intake nozzles 17 from the annular conduit 26 formed between the second  throat 4 of air distribution and the outer casing of the gasifier. Air is admitted to this annular duct 26 by means of a secondary air intake valve 15.

At the base of the gasifier 1 an endless screw conveyor 19 is located to eliminate the mixture of ashes ash that is left at the end of the gasification process. The ashes are discharged by means of a valve rotary 20 with shut-off of the air passage that has a sliding gate valve 21 on it.

The gas produced in the gasifier is removed by means of discharge tubes 18, which preferably they are maintained at an acidic network pressure, that is, less than the atmospheric pressure, by use of a gas suction fan (Figure 2).

The upper part 6, 7, 8, 5 of the gasifier 1 operates similarly to a conventional gasifier of current  descending, while the lower part 14 of the gasifier reactor 1 operates similarly to a gasifier of pyrolyzed carbonaceous upstream material.

The cross-sectional area of the first and second oxidation zones 8, 14 is smaller than that of the area of fuel storage 6 and the pyrolysis zone 7. In order to maintain a uniform distribution of temperatures across these zones, the cross-sectional area of the reduction zone 5 is less than the

 of the first and second oxidation zones 8, 14.

In the gasification process it is preferred to use briquettes or fuel pellets 11 (such as biomass or residual carbonaceous materials) of uniform tamalium, in order to achieve a uniform distribution of air in the throat section above the reduction zone 5. It is also preferred that the maximum diameter of the fuel briquettes are not larger than one eighth of the narrowest part of gasifier 1, in order to avoid

 formation of bridges in the first oxidation zone 8 above the throat 2.

Thermocouples (not shown) can be provided along the gasifier in order to provide the monitoring of the gasification process. A bridge breaker and / or a vibrator can also be provided. (not shown) to allow the destruction of any bridge formed in the first oxidation zone 8 by above throat 2, or to prevent the accumulation of ashes. The spit and / or the vibrator may be

 incorporated into the external section of the upper part of the gasifier 1.

The gasifier 1 shown in Figure 1 is operated continuously after initial ignition and start-up, which It usually takes about 5 to 15 minutes, depending on fuel consumption.

Biomass and / or residues (carbonaceous fuel) of a dense or densified nature are loaded into the gasifier 1 from the upper fuel valve 22. After the solid fuel load is completed, the  fuel valve 22 and the ash discharge valve 21 temporarily stop and close tightly, and the gas suction pump (Figure 2) attached to the discharge tube 18 is started, so that the reactor reaches a pressure of approximately 5 to 10 mbar below the atmospheric pressure, at which time that the primary intake air is introduced into the oxidation zone 8 by means of the annular conduit 23, by the opening of control valves 9 and 25. A gas burner is provided as an ignition device (no

 shown) located in the annular conduct 23, in order to ignite and heat the fuel in the oxidation zone 8 until combustion starts.

The distribution of the air intake nozzles 12 and 24 allows the homogeneous penetration of the air into the area of oxidation 8 to facilitate combustion of the fuel by achieving uniform high temperatures (> 1,000 ° C).

The external ignition stops once a temperature of 8 has been established in the first oxidation zone 8

 operation above 1,000 ° C. Simultaneously, the perforated jacket 3 can be activated for catalysis by the use of a suitable metal-based catalyst to allow the hot product gas to pass through it. In the gasifier 1, this internal microporous catalysis arrangement allows to produce a product gas 13 free of tar, before the gas leaves the gasifier 1. The operating temperature of the first oxidation zone, and with it the amount of gas leaving the gasifier, are subsequently controlled by increasing or

 reduction of the air intake 9. By controlling the air intake 9, 15 and 25, the gasifier 1 can operate efficiently at a capacity as low as 20% of its maximum capacity.

The high temperature reached in the first oxidation zone 8 results in a temperature of approximately 400 to 600 ° C in the pyrolysis zone 7, and approximately 100 ° C in the drying zone 6, by radiation of rising heat.

 During the pyrolysis, which may take about 20 minutes, the dense fuel 11 of uniform size releases gases Reliable and forms a pyrolyzed carbonaceous material without the supply of oxygen. The following reactions are Typical among those that take place in the pyrolysis zone:

Formation of the pyrolized material:

0.17C6H1005 C + 0.85H2 AH3ooK = -80 kJ / g mol

 Gas water displacement:

CO + H20 -gt; CO2 4 'H2 AH3OOK = -33 kJ / g mol

Methane Formation:

CO + 3H2 -gt; CH4 + H2 = -205 kJ / g mol

AH3OOK

CO2 + 4H2 - * CH4 + 2H20 AH3OOK = -192 kJ / g mol

2C0 + 2H2 CH4 + CO2 H298K = -247.3 kJ / mol

Then, the pyrolyzed carbonaceous material is dragged by gravity due to its own weight to the first zone of oxidation 8 and then to reduction zone 5, where reactions take place at high temperatures 5 exothermic and endothermic, respectively.

The following reactions are typical among those that take place in the oxidation zone 8.

Partial oxidation:

C +% 02 CO AH298K = -268 kJ / g mol

CO +% 02 —gt; CO2 = -285.0 kJ / g mol

AH298K

10 H2 + IA 02 -4 H20 AH298K = -241.8 kJ / g mol

An advantage of the operation of the oxidation zone 8 at a temperature of at least 1,000 ° C is that the tar of the pyrolysis gases produced in the pyrolysis zone 7 can be cracked to some extent to produce hydrocarbons of shorter chain length.

In the reduction zone 5 (often also called the gasification zone), the biomass is converted into gas 15 product by reacting with hot gases from areas above 6, 7 and 8.

The following reactions are typical among those that take place in the reduction zone 5:

Methane Formation:

C + 2H2 —gt; CH4 H298K = -74.9 kJ / mol

Boudouard reaction:

20 C + CO2 2C0 AH298K = -172.5 kJ / mol

Water gas reaction:

CO2 + H2 -gt; CO + H2O H298K = -41.2 kJ / mol

C + H2O <- CO + H2 = -131.3 kJ / mol

AH298K

The gases produced by these areas are then aspirated through the jacket 3 with perforations, which can be

25 fill for a highly active microporous catalysis in the wall surrounding the reduction zone of 5, and leave the gasifier through the discharge tube 18. The use of the perforated part 3 of the wall surrounding the area of reduction 5 allows the residual tars of the product gases to be cracked. It also reduces the amount of ashes and particles collected by the product gases, particularly in the second zone of oxidation 14, and are transported out of the gasifier 1.

30 The particles of remaining pyrolized material, which have not been completely gasified in the reduction zone 5, enter the second oxidation zone 14 for secondary combustion and gasification of any material pyrolyzed that remains in the ashes (by reactions similar to those that occur in the first zone of oxidation 8). The product gas formed in the secondary combustion chamber 14 is directed upwards to the discharge 18 due to the negative pressure applied in discharge 18. The amount of secondary oxidation

35 required depends on the content of pyrolized material remaining in the ashes of the fuels. The fuels with a high ash content, such as sewage sludge, leather waste, sludge from oil waste, household waste (RDF), bone meal, chicken manure and livestock, they usually result in a low conversion of carbon in conventional gasifiers because the Ashes isolate part of the carbon in the main oxidation zone. In the gasifier of the present invention,

40 controls the amount of secondary oxidation in the second oxidation zone14 by the amount of air admitted by the secondary air intake valve 15.

Secondary oxidation zones typically operate between 650 and 850 ° C. Mixtures of combustible gases hot (at about 450 ° C) leave the gasifier 1 through the discharge pipe 18, after passing through zone 3 peiforada for catalysis. In Figure 2, the product gas, which may contain a small amount of tar

45 (less than 20-50 mg / m3) and particulate matter, is discharged to a cyclone to remove particles and fly ash and then to one or more heat exchangers and gas-water scrubbers with gas filters final for subsequent treatment, such as the precipitation of tars or moisture in the product gas.

During normal operation of the gasifier 1, the ash screw 19 and the rotary valve 20 operate continuously at a rotational speed such that slag is removed from the reactor so that the

gasification process. The mode of operation of the ash worm screw 19 depends on the ash content of biomass and / or gasified waste.

It is preferred that the gasifier be operated in such a way that the carbon content of the ashes and slags removed from the gasifier is less than 3%.

5 Figure 2 illustrates a gasification system comprising, in series: the gasifier of the invention, a scrubber water, a double polymer filter unit that works in tandem, a fan, a polymer filter unit additional and means for the output of the product gas for power generation.

If necessary, the gas from the water washer may also not pass through the first double unit polymer filter, which preferably consists of two polymer box type filters (this can happen during  the start when the tar content is high). During normal operation, while the gas is passing through one of the box type filters, the polymer is regenerated in the second box type filter by means of the blown with hot exhaust gas from the internal combustion engine. Regeneration can be performed at 80 ° C, while gas cleaning is performed at a temperature below 40 ° C. During the regeneration, that in the second box-type filter uses a polymer, the exhaust gases are also cleaned by absorption

15 by the polymer and the matter in the form of particles is also retained.

This tandem filtration is repeated at the fan outlet, where the pressure is high, which causes more tar and moisture condensation in the second double polymer filter unit, which carries out the water absorption / tar. There are limitations on the temperature of the gas before it can be fed to the Internal combustion engine. The preferred temperature is about 40 ° C. Therefore, the gas coming

 The fan outlet may have to be cooled. This facilitates the removal of tar and moisture by the microporous polymer of the box-type filter at the fan outlet.

The invention is now illustrated in a non-limiting manner with respect to the following examples.

Example 1 - Gasifier operation method according to the invention.

1. Start.

25 The start-up stage includes all the operations required until the regime status is reached when the Gas quality for the engine is stable and without interruptions. A few batches of biomass fuel previously Heavy weights are loaded into the hopper to a predetermined level. Then, the air fan and the pump are connected water washer circulation. The fuel is ignited on the grill using a cigarette lighter solid fuel °.

 2. Gasifier operation.

The measured data are the fuel flow, the gas flow, the gas composition, the temperature and the Pressure. With an analog-to-digital converter, the input air temperatures, the area of drying, the pyrolysis zone, the exit of the throat and the scrubber. Load losses were also measured in the outlet of the gasifier and water washer. Through a gas flow meter located after the fan

The aspiration of the product gas flow rate was measured. From the gas samples taken at the outputs of the gasifier and water washer, the amount of tar and condensate in the product gas was determined.

Wood chips and pyrolized carbonaceous material were placed in the respective trays of the box-type filter, clean and dry, for use as filters. The gas flow meter was regulated for the required flow rate. Be the air fan was started and then the circulation pump (the water washer pump) was connected on the side  of the water tank. Then, the pilot lighter was ignited to ignite the product gas. The flow rate of product gas through the gas flow meter located after the suction fan. It used a circulation fan (gas accelerator fan) to provide the suction effect that would be exerted by the engine coupled to the gasifier, in order to remove the product gas from the gasifier, through the scrubber, to the chimney, where it was wanted after its ignition by means of a pilot burner. The

45 temperature in six different places by means of thermocouples, and the data was recorded in a computer.

3. Gas cleaning.

A U-shaped device is used to collect tar and condensate, and to clean the samples of gas for analysis. Basically, the U-shaped device consisted of a probe for sampling 5 mm diameter stainless steel attached to a plastic tube. This contained two Pyrex tubes in the form of  quot; in series to capture tar and moisture. The first separator contained spherical glass beads of a smaller diameter to provide a large surface area for the wet product gas, while the second separator contained silica gel between two pieces of glass wool). To extract the gas through the tube samples a vacuum pump (AEI type BS 2406, 0.25 HP) was used. Between the U-tubes and the vacuum pump is He placed a rotameter (MEG Fischer, 10 Umin). The gas flow time through the tube was recorded at a flow rate of

55 constant gas, to find the tar content of the product gas.

4. Stop.

The stop procedure included all the actions to close the gasifier in a safe way. He computer, water washer, gas nozzles, circulation fan and exhaust fan the boiler stopped in an orderly sequence, using a burner as a residual effluent gas a burner

 secondary natural degas until no combustible gas was produced.

5. Data processing.

For the complete mass balance, the cleaning procedure included all the necessary procedures for Collect tar, carbon, ashes and condensate. After the reactor was cooled, the amount of ashes and pyrolized material by collecting them in the ash chamber. By

 Finally, the upper plate of the gasifier was opened to carefully remove and check the entire cargas bagasse from an: unused sea. The average fuel feed rate was calculated, dividing the cargas bagasse from Total sugar consumed by the total operating time of the gasifier.

6. Fuel preparation.

In the gasification the consistency of the biomass fuel was important, in order to achieve a flow

 continuous through the reactor and to provide a reliable product gas composition and calorific value for downstream energy conversion procedures. Moreover, the fuel densification of biomass reduced the size of the reactor, while the shape and size of the densified fuel reduced the fluctuations in gas and fuel flow rates, as well as subsequent product quality. For the Biomass fuels that are already dense, such as wood chips, although the additional densification does not

 scriptural, if desirable. However, for fuels with large variations in content and low bulk density, such as urban solid waste, is absolutely inevitable. Therefore the waste urban solids, after the removal of metals and glass, or are heat treated to obtain a Powder rich in cellulose or crushed and then briquetted to densify the fuel.

When the material to be gasified is liquid, such as oil refinery sludge, or it can be dried to

 to obtain a solid material or it can be connected with a solid vehicle, preferably biomass. One such Biomass used was bone meal that contains large amounts of calcium. Therefore, it is Call remove the sulfur of the oil by the formation of calcium sulfate.

7. Gas analysis.

To analyze the gas samples, a gas chromatograph (Shimadzu GC-8A) was used, using helium as a gas

 vehicle. Gas chromatography (GC) had dual columns (chromosorp 101 and molecular sieves) and a thermal conductivity detector. Table 4.1 provides the parameters that influence time and amount of retention of gases for each column. At the same time, the gas was passed through the apparatus in U-shaped tube to find the amounts of tar and condensate in the wet gas produced. Occasionally, throughout the experiment the humidity of the air in the vicinity of the test apparatus was measured ()  to make exact calculations of the mass and energy balance.

Example 2 - Results of gasification with several solid feeds.

Table 2A Fuel inlet

Sludges from Waste Shells

COMPONENTS

sewage deavell ana waste SIZE ° (mm) 35.0x10.0x5.0 17.8x16.5x8.5 50.0x30.0x8.5 70.0x50.0x50 Densidadabs. (kg / m3) 315.04 944.84 836.63 945.13

Clear density (kg / m3) 230.72 319.14 250.28 537.30 C (%) 39.48 46.76 43.43 43.59 H (%) 6.19 5.76 6.08 6.95 0 (%) 25.46 45.83 46.29 32.28 N (%) 3.93 0.22 0.67 10.84 S (%) 1, 45 0.67 0.43 1.45 Ashes (%) 23.51 0.77 3.11 4.89 Moisture content (%) 11, 75 12.45 14.87 11, 23 Materiavolatil (%) 53.48 62.70 64.79 65.75 Carbon fiber (%) 11, 27 24.08 17.24 18.23 HHV (IGT) (MJ / kg) 17.86 18.08 17.20 20.54 HHV (data) (MJ / kg) 17.14 17.36 16.43 19.93

Table 2B Gasifier outlet

Product gas

H2 02 N2 CH4 CO CO2 C2112 C2116 GCV

(Dry) (Dry) (Dry) (Dry) (Dry) (Dry) (Dry) (Dry) (Dry) Kind of

(%) (%) (%) (%) (%) (%) (%) (%) (MJ / N1113)

fuel Wastewater 9.25 1, 28 63.04 1, 83 13.39 9.63 1, 13 0.43 4.82 Hazelnut 13.13 0.93 53.33 2.18 20.66 9.52 0.15 0.11 5.40 Wood 16.58 0.07 53.38 2.04 14.32 13.22 0.27 0.13 5.11 Leather 10.12 0.28 56.39 1, 11 21, 43 10.16 0.23 0.28 4.92

Table 2C Emission values of combustion gases (mg / m3)

NO SO2 NO2 NO NH2 H2S HCN HF HCI Residual sludge 14-45 102-11 2 indications 22-49 NA NA NA NA NA Cascarasdeavel wool 10-15 20-70 signs 12-25 NA NA NA NA NA Wood waste 8-12 13-24 signs 11-27 NA NA NA NA NA Waste waste 8-14 1-7 1-2 4-12 NA NA NA NA NA

2D table. Temperature distribution

Temperature

Temperature Temperature Temperature Temperature

almotor input

of the throat depir Desiccated analysis of the product

T5 (° C)

T1 (° C) T2 (° C) T3 (° C) T4 (° C)

Wastewater 1 .100 500 150 300 35 Wool hazel 1 .250 560 170 320 40 Wood 1 .150 500 130 280 30 Leather 1,280 590 180 350 45

Example 3 - Results of gasification with various feeds. Table 3A Fuel inlet

Bone Waste from Clinical Waste

RDF MSW COMPONENTS *

thermally treated olive tires SIZE ° (mm) 1, 5x0.5x1, 5 70x50x70 1x3x1 10x20x10 Density abs. (kg / m3) NA 897.43 NA NA Clear density (kg / m3) NA 502.16 NA NA C (%) NA 48.00 46.70 NA H (c / 10) NA 5.95 6.20 NA 0 (%) NA 32.46 29.90 NA N (%) NA 1, 54 0.74 NA S (%) 1, 98 0.48 0.30 NA Ashes (%) 3.62 11, 87 16.90 4.5 Moisture content (%) 1, 20 10.11 5.42 6.5 Materiavolatil (%) 65.78 58.71 61, 11 58.00 Carbon fixation (%) 29.40 19.31 16.57 31.00 HHV (IGT) (MJ / kg) 35.01 18.03 20.25 23.25 HHV (data) (MJ / kg) 35.14 17.50 20.22 NA

Table 3B Gasifier outlet

H2 product gas (Dry)

02 (Dry) N2 (Dry) CH4 (Dry) CO (Dry) CO2 (Dry) C2H2 (Dry) C2H6 (Dry) GCV (Dry)

Fuel type (%)

(%) (%) (%) (%) (%) (%) (%) (MJ / Nm3)

Waste of tires 1 0, 60

1, 01 40, 06 2, 80 25, 1 3 1 9, 53 0, 98 0, 71 6, 77

Olive Bones 1 0, 01

1, 80 61, 1 0 2, 50 1 2, 90 1 0, 1 0 1, 30 0, 1 7 5, 04

RDF-MSW 1 2, 1 5

1, 20 52.00 2, 73 1 8, 1 7 1 2, 23 1, 09 0, 43 6, 05

Clinical waste

Table 3C Emission values of combustion gases (mg / m3) NO SO2 NO2 NO NH2 H2S HCN HF HCI Residuosde Neurnaticos NA NA NA NA NA NA NA NA NA Bones of olive 5 7 trace trace NA NA NA NA NA RDF-MSW NA NA NA NA NA NA NA NA NA Residuosclinicos

NANA NA NA NANANANANA

heat treated

3D table. Temperature distribution

Temperature Temperature Temperature Temperature Temperature of the throat of the desiccated desirolysis of the gas

T1 (° C) T2 (° C) 13 (° C) Is (° C) Ts (° C)

Residues of

1300 700 300 450 42

tires

Bones of

1 1 50 450 140 250 37

olive

RDF-MSW 1210 600 230 300 40

Waste

1200 610 240 300 40

clinics

* RDF / MSW: Urban Solid Waste

Conclusion

5 As shown in Tables 2A and 2B, operations provided good control with all fuels of the temperature, providing in the first oxidation zone a throat temperature of about 1,000 ° C The properties of the product gas were excellent, providing in all cases a good Composition of the fuel for later combustion. Particularly, all fuels are characterized by having 6 megajoules / m3, more than the minimum of 4 nnegajoules / m3 necessary for combustion in a

10 combustion engine.

As shown in Tables 3A and 3B, this is suitable for a clean ignition at providing emissions. casualties, for example:

NO (5 mg / m3) and SO2 (7 mg / m3) and levels of evidence for NO2 and NO.

Example 4 -Preparation of the polyhipe polymer for use in a filter that is not in accordance with the invention.

15 The composition of the oil and water phases is given below:

Oil phase: Styrene monomer: (78-XYZ)% Monomer ° of 2-vinylpyridine: X% 2-ethylhexyl acrylate monomer: Y%

20 Soluble initiator in the oil phase: Z% Divinylbenzene (crosslinking agent): 8% Sorbitan mono-monooleate (Span 80 inorganic surfactant): 14%

Aqueous phase: Water with a content of Z% potassium persulfate.

The preferred phase volume of the aqueous phase is 80-95%, more preferably 90-95%.

25 The inclusion of the 2-vinylpyridine monomer in high concentrations resulted in the rupture of the emulsion. Thus, The preferred value of X is between 5-10%.

The use of 2-ethylhexyl acrylate is to make the microporous polymer elastic. The elasticity of the polymer It results in better absorbency of nnecanic shock and good abrasion characteristics. Elasticity It is also (Ail to improve the water uptake capacity of the hydrophilic polymer. The preferred value of the

The concentration of 2-ethylhexyl acrylate is up to Y = 30%, but more preferably, Y = 15%.

The aqueous phase and / or the soluble initiator in the oil phase are present in an amount of Z = 0-1%. The initiator of the oil phase is present when a sulfur-containing aqueous phase initiator is not used (persulfate of potassium).

The preparation of the emulsion was carried out in a batch mixer from an oil phase and a phase

The aqueous emulsion was dosed at a predetermined rate, while stirring at a rate of constant rotation The dosing speed, deformation speed and the speed of mixing, depending on the volume of the respective phases, the diameter of the batch mixer and the impellers, the rotation speed of the impellers and the homogenization time.

In order to eliminate the differences in performance of the different mixing conditions, the mixing 40 dryness by means of:

Dosing rate: RD = / tD

GOES

Deformation rate during dosing: RE = VA I (tDVO)

Mixing Rate: Rm = D1 / Do

Where: VA = Volume of the aqueous phase added during the period of time to.

5 Vo = Volume of the oil phase placed in the batch mixer. D1 = Diameter of the impellers. Do = Batch mixer diameter. 0 = Rotation speed.

Also tH was defined as the homogenization time and tT as the total mixing time.

10 1-r

 = tD 111

In a 8.5 cm diameter mixing tank two flat vane impellers (8 cm in diameter and 1.4 cm) were used cm wide) The impeller spacing was 1 cm. 25 ml of the oil phase was placed at the bottom of the tank and 225 ml of the aqueous phase were dosed, using 4 feeding points. Phase temperature aqueous oscillate from -1.0 to 80 ° C.

In the preparation of the polymer with vinyl pyridine, polymerization was carried out at 40 ° C for 8 hours and then at 50 ° C for 8 hours and finally another 8 hours at 60 ° C. This ensured that the emulsion would not destabilize. during polymerization. It has been discovered that during the "drying phase"; the polymers should not dry excessively. Excessive drying results in the reduction of the polymer's water absorption capacity, as well as to the reduction of the water collection rate. Typically, the water absorption capacity of these

20 polymers was 10-12 times their own weight.

Claims (26)

1.-A gasifier (1) for the gasification of biomass and waste to produce a fuel effluent, which understands: a) a fuel valve (22), for loading solid fuel (11) into a first oxidation zone (8);  b) a first throat (2), which defines the lower edge of the first oxidation zone (8); c) a second throat (4), which defines the lower edge of a second oxidation zone (14); d) a reduction zone (5), which joins the first oxidation zone (8) with the second oxidation zone (14); Y e) two vortex discharge tubes (18), located opposite (in the reduction zone), for the effluent  fuel; wherein the flow of gas in the first oxidation zone takes place in the same direction as the flow of fuel, and the flow of gas in the second oxidation zone takes place in the opposite direction to the flow of fuel, and characterized in that an area (3) with a catalyst is located below the reduction zone (5)  microporous, in the form of a perforated jacket (3) for catalysis, which joins the first oxidation zone (8) with the tubes download (18). 2. A gasifier (1) according to claim 1, further comprising a pyrolysis zone (7) above the first oxidation zone (8), and a fuel storage and drying zone (6) above the zone pyrolysis (7).  3. A gasifier (1) according to claims 1 6 2, further comprising air distribution nozzles (12, 17) to provide air to the first and second oxidation zones, wherein said nozzles are provided in the first throat (2), the upper half of the reduction zone (5) and the second throat (4). 4. A gasifier (1) according to any of claims 1 to 3, which further comprises a central assembly of air nozzles (24) above the first oxidation zone (8) to supply air to the first zone of  oxidation (8). 5. A gasifier according to any of the preceding claims, which further comprises a mechanism of discharge without grill (19) below the second oxidation zone (14). 6. A gasifier according to claim 5, wherein the unloading mechanism without grill comprises a worm conveyor (19).  7. A segt gasifier: in any of the preceding claims, wherein the first and / or the second throat (2, 4) are angled at an angle (10, 16) between 10 and 40 ° with respect to the horizontal axis. 8. A gasifier (1) according to any of the preceding claims, wherein the first throat (2) and the Second throat (4) are located symmetrically with respect to each other. 9. A gasifier (1) according to any of the preceding claims, further comprising means  incorporated into the discharge tubes (18) in order to keep the pressure in the gasifier (1) below the pressure atmospheric 10. A gasifier (1) according to any of the preceding claims, wherein the area of the semi Transverse of the first and second oxidation zones (8, 14) is smaller than that of the zones of fuel storage (6) and pyrolysis (7).  11. A gasifier (1) according to claim 10, wherein the semi-transverse area of the reduction zone (5) is less than that of the first and second oxidation zones (8, 14). 12.-A method for the gasification of solid fuel to produce a fuel effluent, which uses a gasifier as described in any one of claims 1 to 11, comprising the steps of: 1) partially oxidize a biomass fuel in the first oxidation zone (8) to produce a  pyrolized material; 2) reduce the pyrolyzed material in the reduction zone (5) to form ashes; 3) oxidize aim more any residue in the ashes of pyrolized material, in the second oxidation zone (14); 4) extract the fuel effluent produced in the previous stages, by means of the discharge pipe (18); where the flow of gas in the first oxidation zone takes place in the same direction as the flow of fuel, and the flow of gas in the second oxidation zone takes place in the opposite direction to that of the flow of fuel,  13. A method according to claim 12, wherein the extraction is carried out through a microporous catalyst (3), preferably in the form of a perforated jacket (3) for catalysis. 14. A method according to any of claims 12 6 13, wherein the first oxidation zone operates at a temperature greater than 850 ° C, preferably at least 1,000 ° C. 15. A method according to any of claims 12 to 14, which comprises passing through the  catalyst (3) the combustion gases of the first oxidation zone, to produce a tar-free gas. 16. A method according to any of claims 12 to 15, wherein the temperature of the first zone of Combustion is controlled by regulating the air intake (9). 17. A method according to any of claims 12 to 16, wherein the reduction zone operates at a temperature between 600 and 900 ° C.   18. A method according to any of claims 12 to 17, wherein the second oxidation zone operates at a temperature between 700 and 800 ° C.   19. A method according to any of claims 12 to 18, which comprises pyrolizing the fuel in the area of pyrolysis to form a pyrolyzed carbonaceous material, which dries and moves by gravity to the first zone of oxidation and then to the reduction zone.  20.-A method according to claim 19, wherein the temperature in the pyrolysis zone is 400-600 ° C and the temperature in the drying zone is in the environment of 100 ° C. 21. A method according to claims 19 or 20, wherein the tar remaining in the pyrolysis gases is cracks in the first oxidation zone. 22. A method according to any of claims 12 to 21 for the gasification of biomass, such as a  liquid residue, for example residual oil or oil sludge, which is absorbed inside the pores intraparticle or interparticle of a suitable fuel vehicle. 23.-A method according to claim 22, wherein the fuel vehicle has a high internal porosity and preferably it is in fibrous form to provide considerable interparticle porosity. 24. A method according to claims 22 6 23, wherein the liquid residue is mixed with the vehicle and is  briquette, in order to densify the composite fuel. 25. A method according to claims 22 to 24, wherein the suitable fuel vehicle is selected from sawdust, crushed bone waste from slaughterhouses, bread / food waste, urban waste, sludge Dried sewage, chopped straw, rapeseed meal, sugarcane bagasse. 26.-The use of a gasifier, and a method, in the gasification of a solid fuel as defined in what  above, to generate combustible gases for use in energy generation.  Figure 1. Gasifier (1)   19 INPUT OF FUEL GAS PRODUCT CYCLONE AND COOLER OF GAS CYCLONES AND COOLERS DOUBLE TANK OF WATER OF RECYCLING DISCHARGE OF ASHES VENT1ADOR FROM ASPIRAC ION OF GAS